EP0479286A1 - Procédé pour purifier des gaz contenant des dioxines et des furanes - Google Patents

Procédé pour purifier des gaz contenant des dioxines et des furanes Download PDF

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Publication number
EP0479286A1
EP0479286A1 EP91116863A EP91116863A EP0479286A1 EP 0479286 A1 EP0479286 A1 EP 0479286A1 EP 91116863 A EP91116863 A EP 91116863A EP 91116863 A EP91116863 A EP 91116863A EP 0479286 A1 EP0479286 A1 EP 0479286A1
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EP
European Patent Office
Prior art keywords
adsorbent
dioxins
furans
activated coke
gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP91116863A
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German (de)
English (en)
Other versions
EP0479286B1 (fr
Inventor
Michael Dr. Rer.Nat. Berger
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
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Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP0479286A1 publication Critical patent/EP0479286A1/fr
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Publication of EP0479286B1 publication Critical patent/EP0479286B1/fr
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • B01D53/70—Organic halogen compounds

Definitions

  • the invention relates to a process for purifying exhaust gases containing polyhalogenated compounds by means of adsorption, the adsorbent loaded with pollutants being transported to further processing or deposition under inert gas conditions.
  • Flue gas cleaning in thermal power stations and waste incineration plants are used to remove pollutants such as Mercury, dioxins and furans adsorption stages with activated carbon, activated coke or lime-coal mixtures are used as adsorbents.
  • activated coke or lime-coal mixtures are used as adsorbents.
  • hearth furnace coke made from lignite can be used as activated carbon.
  • Activated coke can e.g. can be obtained as shaped active coke from hard coal.
  • Lime-coal mixtures include available as merchandise.
  • the adsorbent loaded with pollutants after flue gas cleaning must be temporarily stored or transported before its disposal. The disposal itself can be carried out in compliance with high safety and environmental requirements by incineration or landfill.
  • the invention is therefore based on the object of designing a method of the type mentioned at the outset such that decontamination of the adsorbent laden with pollutants, in particular destruction of dioxins and furans, is achieved in an economical manner.
  • the present invention is based on the knowledge that when the adsorbent is transported under inert gas protection, there are ideal conditions for supplementary destruction of dioxins and fur, provided that heating and cooling zones are switched on in the transport route. Oxygen deficiency conditions are already in place through inerting. Since the transported adsorbent has a relatively high surface area and, in addition, the adsorbent is mixed during transport, extensive destruction of the dioxins and furans is achieved even with short heating and cooling phases. For these reasons, you can get by with relatively low temperatures. Accordingly, the adsorbent is preferably heated to temperatures of approximately 250 to 450 ° C. Heating and cooling can be done using standard radiation or conductivity processes.
  • infrared radiators can be used or the transport lines can be heated or cooled from the outside by means of a heating or cooling medium.
  • liquid nitrogen or cryogenic nitrogen gas is injected into the transport path to cool the adsorbent.
  • Activated carbon, activated coke or a lime-coal mixture is preferably used as the adsorbent.
  • These adsorbents can be used to separate harmful gases such as S0 2 , HCl, HF, H 2 S, NH 3 , basic amines and gaseous heavy metals, especially mercury.
  • harmful gases such as S0 2 , HCl, HF, H 2 S, NH 3 , basic amines and gaseous heavy metals, especially mercury.
  • fine dust and thus the particle-bound pollutants such as cadmium and lead attached to it are filtered out of the exhaust gas to be cleaned.
  • These adsorbents particularly well retain dioxins and furans, which are generated, for example, in waste incineration plants.
  • the transport of the adsorbent can be done mechanically, e.g. by means of an assembly line. According to a preferred embodiment of the invention, however, the adsorbent is transported pneumatically by means of nitrogen. In this way, two tasks can be performed simultaneously, namely transport and inertization of the adsorbent. In addition, if the adsorbent is cooled by injecting liquid nitrogen or cryogenic nitrogen gas, the resulting nitrogen gas can be used simultaneously as an inerting and transport medium.
  • the adsorbent is freed from volatile and desorbable substances after the heating of the adsorbent by means of a solid-gas phase separation.
  • the adsorbent can be fed to a cyclone after a heating zone, in which mercury, condensates, etc. are separated from the adsorbent.
  • the separated pollutants are preferably fed to flue gas cleaning, which has suitable sinks for these pollutants.
  • a conventional flue gas cleaning system 20 for example a laundry
  • an activated coke filter 3 for example a denitrification stage 21, for example a shaped activated carbon filter.
  • the cleaned exhaust gas is finally drawn off via a chimney 22.
  • Lignite coke which has very good adsorption properties, in particular with regard to polyhalogenated compounds such as dioxins and furans, serves as active coke. Used activated coke, ie loaded with pollutants, is drawn off via line 5 and fed to a metering container 6.
  • Fresh activated coke is refilled into the activated coke filter 3 via a feed container 4.
  • the used activated coke contains the polyhalogenated compounds, in particular dioxins and furans, filtered out of the exhaust gas of the waste incineration plant 1 in high concentration.
  • a pneumatically operated by means of nitrogen gas delivery line 7 is used, which is supplied with nitrogen gas via a gas line 8.
  • the nitrogen is provided in a liquid gas container 9.
  • the liquid nitrogen is converted into the gaseous state in an evaporator 10 in order to be able to operate the pneumatic delivery line 7.
  • the nitrogen gas not only serves as a transport medium for the activated coke, but also provides the inert gas atmosphere required to destroy the dioxins and furans. This also prevents possible fire hazards.
  • a heating zone 11 and a cooling zone 12 are installed in the delivery line 7.
  • superheated steam which was generated by means of the flue gas from the waste incineration plant 1, is brought into indirect heat exchange with the activated coke via a heat exchanger 13.
  • the hot activated coke is then fed to a cyclone 14, in which the active coke is freed of volatile and desorbable substances by means of solid-gas phase separation.
  • the separated pollutants are drawn off via line 16 and fed to the flue gas cleaning system 20 of the waste incineration plant 1, which has suitable sinks for these pollutants.
  • the activated coke then arrives at the cooling zone 12, in which the hot activated coke is cooled suddenly by means of liquid nitrogen injection.
  • the liquid nitrogen is removed from the liquid gas container 9 and fed to the cooling zone 12 via line 15.
  • the nitrogen evaporated in the cooling zone 12 is separated off and returned to the gas line 8 via line 18.
  • the returned nitrogen is mixed with the nitrogen gas coming from the evaporator 10 and is used as a transport medium for the active coke transport in the delivery line 7.
  • the liquid nitrogen can, for example, be introduced into a hollow wall of the delivery line 7.
  • the evaporated nitrogen is then withdrawn from the hollow wall and fed to the gas line 8 in order to serve as a transport medium for the activated coke.
  • the cyclone 17 for separating the nitrogen from the activated coke transport is not necessary in this case. Due to the heating and subsequent cooling of the activated coke under inert gas conditions, the dioxins and furans are destroyed. The mixing processes as a result of the active coke transport have a beneficial effect on the degradation reactions.
  • the fact that the activated coke is present in the delivery line 7 with a large surface area also accelerates the breakdown of the dioxins and furans. Therefore, relatively short heating and cooling times are sufficient to go far de Destruction of dioxins and furans.
  • the activated coke treated in this way is finally returned to the furnace of the waste incineration plant 1.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Treating Waste Gases (AREA)
EP91116863A 1990-10-05 1991-10-02 Procédé pour purifier des gaz contenant des dioxines et des furanes Expired - Lifetime EP0479286B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE4031646A DE4031646A1 (de) 1990-10-05 1990-10-05 Verfahren zur reinigung polyhalogenierte verbindungen enthaltender abgase
DE4031646 1990-10-05

Publications (2)

Publication Number Publication Date
EP0479286A1 true EP0479286A1 (fr) 1992-04-08
EP0479286B1 EP0479286B1 (fr) 1994-08-31

Family

ID=6415707

Family Applications (1)

Application Number Title Priority Date Filing Date
EP91116863A Expired - Lifetime EP0479286B1 (fr) 1990-10-05 1991-10-02 Procédé pour purifier des gaz contenant des dioxines et des furanes

Country Status (3)

Country Link
EP (1) EP0479286B1 (fr)
AT (1) ATE110581T1 (fr)
DE (2) DE4031646A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1993014862A1 (fr) * 1992-01-25 1993-08-05 British Steel Plc Traitement d'effluents gazeux provenant de fourneaux metallurgiques
EP0574705A1 (fr) * 1992-06-15 1993-12-22 Sumitomo Heavy Industries, Ltd Procédé pour l'élimination de dioxines
EP0693308A3 (fr) * 1994-07-20 1996-08-14 Karlsruhe Forschzent Application d'un lit fixe et procédé pour retenir des composés polyhalogénés

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3426059A1 (de) * 1984-07-14 1986-01-16 Hugo Petersen Gesellschaft für verfahrenstechnischen Anlagenbau mbH & Co KG, 6200 Wiesbaden Verfahren zur abscheidung und beseitigung von organischen schadstoffen, insbesondere von polychlorierten dibenzodioxinen (pcdd) aus rauchgasen
EP0208592A1 (fr) * 1985-06-25 1987-01-14 Hydro-Quebec Procédé pour la destruction de matière organique toxique
EP0284227A2 (fr) * 1987-03-04 1988-09-28 Praxair Canada Inc. Installation et procédé pour la récupération d'hydrocarbures halogénés dans un courant gazeux
DE3813613A1 (de) * 1988-04-22 1989-11-02 Asea Brown Boveri Verfahren zum pyrolysieren von halogenhaltigen, toxischen kohlenwasserstoffverbindungen
DE3827086A1 (de) * 1988-08-10 1990-02-15 Atzger Juergen Verfahren und vorrichtung zur thermischen entkontaminierung von filterstaeuben und anderen reststoffen

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3426059A1 (de) * 1984-07-14 1986-01-16 Hugo Petersen Gesellschaft für verfahrenstechnischen Anlagenbau mbH & Co KG, 6200 Wiesbaden Verfahren zur abscheidung und beseitigung von organischen schadstoffen, insbesondere von polychlorierten dibenzodioxinen (pcdd) aus rauchgasen
EP0208592A1 (fr) * 1985-06-25 1987-01-14 Hydro-Quebec Procédé pour la destruction de matière organique toxique
EP0284227A2 (fr) * 1987-03-04 1988-09-28 Praxair Canada Inc. Installation et procédé pour la récupération d'hydrocarbures halogénés dans un courant gazeux
DE3813613A1 (de) * 1988-04-22 1989-11-02 Asea Brown Boveri Verfahren zum pyrolysieren von halogenhaltigen, toxischen kohlenwasserstoffverbindungen
DE3827086A1 (de) * 1988-08-10 1990-02-15 Atzger Juergen Verfahren und vorrichtung zur thermischen entkontaminierung von filterstaeuben und anderen reststoffen

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1993014862A1 (fr) * 1992-01-25 1993-08-05 British Steel Plc Traitement d'effluents gazeux provenant de fourneaux metallurgiques
EP0574705A1 (fr) * 1992-06-15 1993-12-22 Sumitomo Heavy Industries, Ltd Procédé pour l'élimination de dioxines
EP0693308A3 (fr) * 1994-07-20 1996-08-14 Karlsruhe Forschzent Application d'un lit fixe et procédé pour retenir des composés polyhalogénés

Also Published As

Publication number Publication date
DE4031646A1 (de) 1992-04-09
DE59102730D1 (de) 1994-10-06
ATE110581T1 (de) 1994-09-15
EP0479286B1 (fr) 1994-08-31

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